Oligomerisation process

ABSTRACT

This invention relates to base oils for lubricating compositions. In particular, the present invention provides a process for the selective oligomerisation of C 5  to C 20  alpha-olefins to produce polyalphaolefin oligomers with a molecular weight distribution that is suitable for use in lubricant base oils.

This invention relates to base oils for lubricating compositions. Inparticular, the present invention provides a process for the selectiveoligomerisation of C₅ to C₂₀ alpha-olefins to produce polyalphaolefinoligomers with a molecular weight distribution that is suitable for usein lubricant base oils.

Lubricant compositions generally comprise a base oil of lubricatingviscosity together with one or more additives to deliver properties suchas reduced friction and wear, improved viscosity index, detergency, andresistance to oxidation and corrosion. A lubricant base oil may compriseone or more sources of lubricating oil, referred to as base stocks.

Lubricant base stocks useful in automotive engine lubricants may beobtained as higher boiling fractions from the refining as crude oil orvia synthetic routes, and are classified as Group I, II, III, IV and Vbase stocks according to API standard 1509, “ENGINE OIL LICENSING ANDCERTIFICATION SYSTEM”, April 2007 version 16^(th) edition Appendix E.Group IV refers to polyalphaolefin (PAO) base stocks, which aretypically synthesised by oligomerisation of 1-decene. The principalcomponent of these base stocks is decene trimer, although the dimer,tetramer and pentamer are typically also present in the various basestock blends.

A number of catalytic processes are currently in use for theoligomerisation of alpha-olefins to produce lubricant base stocks.

Ziegler-Natta catalysts are a class of catalysts that comprise titaniumcompounds in combination with an organoaluminium compound. Typically,Ziegler-Natta catalysts used commercially for the polymerisation ofalpha-olefins comprise a titanium complex (such as TiCl₄) together withan organoaluminium compound (such as triethylaluminium) on a magnesiumchloride support.

Metallocene complexes (such as dicyclopentadienylzirconium dichloride,Cp₂ZrCl₂) have also been used as catalysts for the oligomerisation ofalpha-olefins in combination with a methylaluminoxane activator.

It is also known that Lewis acids such as BF₃, AlCl₃ and EtAlCl₂ can beused as catalysts for cationic polymerisation of alpha-olefins inconjunction with an alkyl halide (for instance tent-butyl chloride),alcohol or Brønsted acid.

U.S. Pat. No. 7,527,944 discloses the use of ionic liquids as catalystsfor the cationic polymerisation of alpha-olefins. Ionic liquids are aclass of compounds that have been developed over the last few decades.The term “ionic liquid” as used herein refers to a liquid that can beobtained by melting a salt, and which is composed entirely of ions. Theterm “ionic liquid” includes compounds having both high melting pointsand compounds having low melting points, e.g. at or below roomtemperature. Ionic liquids having melting points below around 30° C. arecommonly referred to as “room temperature ionic liquids” and are oftenderived from organic salts having nitrogen-containing heterocycliccations, such as imidazolium and pyridinium-based cations.

The ionic liquid catalysts disclosed by U.S. Pat. No. 7,572,944 comprisepyridinium or imidazolium cations together with chloroaluminate anions.The use of ionic liquids as polymerisation catalysts is known to providecertain advantages over conventional catalysts. In particular, ionicliquids are generally immiscible with hydrocarbons and thus can beseparated from polyalphaolefin products by phase separation andrecycled. In contrast, conventional Lewis acid catalysts are generallyquenched during the isolation of products.

However, a disadvantage of ionic liquid systems is that the organiccations are spectator ions which play no part in the catalytic reaction,other than to moderate the melting point of the ionic liquid reactionmedium. The organic cations commonly used in ionic liquids are generallyexpensive, and require additional synthetic steps to prepare the desiredcation from commercially available precursors. Specifically, it isusually necessary to prepare an ionic liquid of the formula [cation]⁺Cl⁻in a first step, followed by a second step in which the chloride ionicliquid is converted to a chloroaluminate ionic liquid by reaction withAlCl₃. It would therefore be desirable to identify new systems which maybe prepared more easily and with less expense than chloroaluminate ionicliquids.

A further disadvantage of ionic liquid systems, in common with otherLewis acid catalysts, is that the catalysts are extremely active andthus tend to form undesired highly oligomerised products, therebywasting resources. While the use of dopants to moderate the Lewisacidity of chloroaluminate ionic liquid systems has been investigated,these provide in general only modest improvements.

In the past few years, there has been growing interest in identifyingsustainable sources of hydrocarbons and products derived fromhydrocarbons. Bio-derived feedstocks are a potential resource for thepreparation of lubricants, both to meet consumer demand for “green”products and to reduce dependence of crude oil resources. In particular,natural fats and oils are a potential feedstock for the production oflubricants that are traditionally based on petroleum. Lubricant basestocks have been obtained from vegetable sources such as palm oil, cornoil, soybean oil, sunflower oil and rapeseed oil—generally astriglyceride esters of fatty acids. Free fatty acids from plant sourceshave also been used in the preparation of various synthetic esterlubricant base stocks.

While, lubricants based on vegetable oils and synthetic esters derivedfrom vegetable oils are useful for many purposes, they do not provide anideal substitute for lubricant base oils derived from crude oil. Esterbonds may undergo hydrolysis in the presence of water and may beincompatible with other blending components of lubricants, for examplesome mineral oils. Furthermore, the rheological properties oftriglyceride and synthetic ester base oils may not be appropriate forall applications. It would therefore be useful if processes could beidentified for the conversion of bio-derived feedstocks to conventionalbase stocks, such as polyalphaolefin base stocks.

It is known that olefins may be obtained via the deoxygenation ofbio-derived fatty acids. However, there remains a need for processes toconvert such olefins to PAO base stocks.

Accordingly, there is a need in the art for new processes for theproduction of polyalphaolefin oligomers which overcome one or more ofthe disadvantages of the processes that are known in the art. Inparticular, there is a need for processes which are suitable for theproduction of polyalphaolefin oligomers from bio-derived olefins with aproduct distribution suitable for use as a lubricant base stock.

In a first aspect, the present invention provides a process for thepreparation of alpha-olefin oligomers, comprising contacting an olefinicfeedstock comprising C₅ to C₂₀ alpha-olefins with a liquid complexcatalyst comprising:

-   -   (i) at least one metal halide salt of the formula MX₃, wherein M        is selected from aluminium and gallium, and each X is        independently selected chlorine, bromine and iodine; and    -   (ii) at least one Lewis basic donor ligand containing a donor        atom selected from oxygen, sulphur, nitrogen, phosphorus,        arsenic and selenium;        wherein the molar ratio of the at least one metal halide salt to        the at least one Lewis basic donor ligand is in the range of        from 1:1 to 4:1.

As used herein, the term “liquid complex” or “LC” refers to a class ofliquids that is composed of metallate cations and anions in equilibriumwith neutral species. Liquid complexes are obtained by combining neutraldonor molecules with Al(III) or Ga(III) halides. Without being bound byany specific theory, it is understood from spectroscopic studies thatthe addition of a donor ligand to Al(III) or Ga(III) halides causesdisproportionation of the metal species into cationic and anioniccomplexes which exist in equilibrium with neutral complexes, accordingto the following general schemes (wherein L represents a Lewis basicdonor ligand and χ_(MX3) indicates the mole fraction of MX₃):

2MX ₃+2L→[MX ₂ L ₂]⁺ +[MX ₄]⁻□2[MX ₃ L](χ_(MX3)=0.50)

3MX ₃+2L→[MX ₂ L ₂]⁺ +[M ₂ X ₇]⁻ □[MX ₃ L]+[M ₂ X ₆ L](χ_(MX3)=0.60)

4MX ₃+2L→[MX ₂ L ₂]⁺ +[M ₃ X ₁₀]⁻□2[M ₂ X ₆ L](χ_(MX3)=0.67)

FIG. 1 shows a portion of the ²⁷Al NMR spectra obtained for liquidcomplexes comprising AlCl₃ and acetamide at a molar ratio of 1:1(χ_(AlCl3)=0.50) and 3:2 (χ_(AlCl3)=0.60). The peaks identified in thespectrum correspond to the cationic, anionic and neutral speciesdescribed above.

Liquid complexes are thus distinct from chlorometallate ionic liquids,which consist only of ions, whereas LCs are believed to comprise ionicspecies in equilibrium with neutral species. Furthermore, the activeLewis acidic catalytic species in chloroaluminate ionic liquids isalways the [Al₂Cl₇]⁻ anion, and only its concentration in the ionicliquid can be manipulated. In contrast, in LCs, the reactivity of thesystem depends on the ligands selected and on the molar ratio of ligandsto the metal halide salt (χ_(MX3)). Accordingly, LCs provide muchgreater scope for modulating the reactivity of the system compared tochloroaluminate ionic liquids.

The present inventors have surprisingly found that the use of liquidcomplexes as defined above as catalysts for the oligomerisation of C₅ toC₂₀ alpha-olefins provides an oligomerised product with a molecularweight distribution that is particularly suitable for use as a lubricantbase stock, i.e. consisting predominantly of dimers, trimers, tetramersand pentamers, and with only low levels of undesired highly oligomerisedproducts. The liquid complexes are also immiscible with the oligomericproduct and thus can readily be separated from the product by phaseseparation. Furthermore, separation of the liquid complexes from theoligomeric product is non-destructive for the liquid complexes, whichcan therefore be recycled to the oligomerisation reaction without theneed for purification or regeneration steps. Still a further advantageof the liquid complex systems of the present invention is that cheap,widely available Lewis donor ligands such as urea, thiourea, acetamideand dimethylsulfoxide may be used to prepare the liquid complexes, thusproviding a significant cost saving in comparison to the use ofexpensive ionic liquid cations as described above.

Where M represents aluminium, the molar ratio of the at least one metalhalide salt to the at least one Lewis basic donor ligand is preferablyin the range of from 1:1 to 2:1.

More preferably, where M represents aluminium, the molar ratio of the atleast one metal halide salt to the at least one Lewis basic donor ligandis from about 55:45 (χ_(MX3)=0.55) to about 65:35 (χ_(MX3)=0.65). Stillmore preferably, where M represents aluminium, the molar ratio of themetal halide salt to the at least one Lewis basic donor ligand is about3:2 (χ_(MX3)=0.60).

Where M represents gallium, the molar ratio of the metal halide salt tothe at least one Lewis basic donor ligand is preferably in the range offrom 1:1 to 3:1.

More preferably, where M represents gallium, the molar ratio of thegallium halide salt to the at least one Lewis basic donor ligand is fromabout 55:45 (χ_(MX3)=0.55) to about 75:25 (χ_(MX3)=0.65). Still morepreferably, where M represents gallium, the molar ratio of the galliumhalide salt to the at least one Lewis basic donor ligand is about 3:2(χ_(MX3)=0.60).

In preferred embodiments, M represents aluminium.

X preferably represents bromine or chlorine. Most preferably, Xrepresents chlorine.

In further preferred embodiments MX₃ is selected from AlCl₃ and GaCl₃.Most preferably, MX₃ represents AlCl₃.

In some embodiments of the invention, the metal halide salt having theformula MX₃ may optionally comprise two or more salts having the formulaMX₃.

The at least one Lewis basic donor ligand is preferably selected fromsmall molecule donor ligands having a molecular weight of 500 or less,preferably a molecular weight of 400 or less, more preferably amolecular weight of 300 or less, still more preferably a molecularweight of 200 or less, and most preferably a molecular weight of 100 orless.

In preferred embodiments, the at least one Lewis basic donor ligand isselected from ligands containing a donor atom selected from oxygen,sulphur, nitrogen and phosphorus, more preferably from oxygen, sulphurand phosphorus, still more preferably from oxygen and sulphur. Mostpreferably, the at least one Lewis basic donor ligand is selected fromligands containing an oxygen donor atom.

In further preferred embodiments, the at least one Lewis basic donorligand is selected from the group of compounds consisting of ketones,sulfoxides, phosphine-oxides, ureas, esters, amides, ethers,thioketones, thioureas, thioamides, thioethers, amines, nitriles andphosphines. More preferably, the at least one Lewis basic donor ligandis selected from the group of compounds consisting of ketones,sulfoxides, phosphine-oxides, ureas, esters, amides, ethers,thioketones, thioureas, thioamides and thioethers. Still morepreferably, the at least one Lewis basic donor ligand is selected fromthe group of compounds consisting of ketones, sulfoxides, phosphineoxides, ureas, esters, amides and ethers. Still more preferably, the atleast one Lewis basic donor ligand is selected from the group ofcompounds consisting of sulfoxides, ureas and amides. Most preferably,the at least one Lewis basic donor ligand is an amide or a urea ligand.

In further preferred embodiments, the at least one Lewis basic donorligand is selected from compounds having a formula selected fromR¹—C(O)—R¹, R¹—S(O)—R¹, R²NH—C(O)—NHR², R²NH—C(S)—NHR^(2,) R¹—C(O)—NR²₂, R¹—C(O)—OR¹, (R³)₃P(O) and R¹—CN wherein:

each R¹ independently represents a C₁ to C₁₀ straight chain or branchedalkyl group, preferably a C₁ to C₆ alkyl group, more preferably a C₁ toC₃ alkyl group and most preferably a methyl group;

R² is selected from hydrogen or a C₁ to C₁₀ straight chain or branchedalkyl group, more preferably from hydrogen or a C₁ to C₆ alkyl group,still more preferably from hydrogen or a C₁ to C₃ alkyl group, and mostpreferably from hydrogen or a methyl group; and

R³ represents a C₄ to C₁₀ straight chain or branched alkyl group,

wherein any of R¹, R² and R³ may optionally be substituted by one ormore fluorine atoms.

Examples of suitable C₁ to C₁₀ alkyl groups include methyl, ethyl,propyl, isopropyl, n-butyl, iso-butyl, sec-butyl, tert-butyl, n-pentyl,n-hexyl, n-heptyl, n-octyl, n-nonyl, n-decyl, trifluoromethyl andpentafluoroethyl. Preferred alkyl groups include methyl, ethyl, propyl,isopropyl, n-butyl, iso-butyl, sec-butyl, tert-butyl, n-pentyl, andn-hexyl. More preferred alkyl groups include methyl, ethyl, propyl, andisopropyl. Most preferably, the alkyl group is methyl.

In still further preferred embodiments, the at least one Lewis basicdonor ligand is selected from compounds having a formula selected fromR¹—S(O)—R¹, R²NH—C(O)—NHR², R²NH—C(S)—NHR², R¹—C(O)—NR² ₂ and (R³)₃P(O);more preferably, the at least one Lewis basic donor ligand is selectedfrom compounds having a formula selected from R²NH—C(O)—NHR² andR¹—C(O)—NR² ₂; and most preferably the at least one Lewis basic donorligand is a compound having the formula R²NH—C(O)—NHR², wherein R¹ andR² are as defined above.

Examples of suitable Lewis basic donor ligands in accordance with thepresent invention include urea, N,N′-dimethylurea,N,N′-dimethylthiourea, acetamide, dimethylacetamide, acetone, ethylacetate dimethylsulfoxide and trioctylphosphine oxide. More preferably,the at least one Lewis basic donor ligand is selected from urea andacetamide. Most preferably, the at least one Lewis basic donor ligand isurea.

In some embodiments of the invention, the at least one Lewis basic donorligand may comprise a mixture of two or more Lewis basic donor ligandsas described herein.

Preferred liquid complex catalysts in accordance with the presentinvention comprise AlCl₃ and a ligand selected from urea,N,N′-dimethylurea, N,N′-dimethylthiourea, acetamide, anddimethylacetamide in a molar ratio of AlCl₃ to ligand of from 1:1(χ_(AlCl)=0.50) to 2:1 (χ_(AlCl3)=0.67), preferably in a molar ratio ofAlCl₃ to ligand of from 55:45 (χ_(MX3)=0.55) to about 65:35(χ_(MX3)=0.65), and more preferably in a molar ratio of AlCl₃ to ligandof about 3:2 (χ_(AlCl3)=0.60). More preferably the liquid complexcatalyst comprises AlCl₃ and urea in a molar ratio of about 3:2, or theliquid complex catalyst comprises AlCl₃ and acetamide in a molar ratioof about 3:2. Most preferably, the liquid complex catalyst comprisesAlCl₃ and urea in a molar ratio of about 3:2.

As used herein, the term “olefinic feedstock comprising C₅ to C₂₀alpha-olefins” preferably refers to a hydrocarbonaceous feedstock thatcomprises at least one C₅ to C₂₀ alpha-olefin hydrocarbon. Preferably,the olefinic feedstock comprises at least 50 wt % of one or more C₅ toC₂₀ alpha-olefins, more preferably at least 60 wt % of one or more C₅ toC₂₀ alpha-olefins, more preferably at least 70 wt % of one or more C₅ toC₂₀ alpha-olefins, more preferably at least 80 wt % of one or more C₅ toC₂₀ alpha-olefins, more preferably at least 90 wt % of one or more C₅ toC₂₀ alpha-olefins, and most preferably at least 95 wt % of one or moreC₅ to C₂₀ alpha-olefins. In some embodiments, the olefinic feedstock maycomprise at least 98 wt % of one or more C₅ to C₂₀ alpha-olefins, or atleast 99 wt % of one or more C₅ to C₂₀ alpha-olefins. The remainder ofthe olefinic feedstock may suitably be composed of other olefins,paraffins, or a mixture thereof.

In preferred embodiments, the olefinic feedstock comprises at least 50wt % C₆ to C₁₈ alpha-olefins, more preferably at least 60 wt % C₆ to C₁₈alpha-olefins, more preferably at least 70 wt % C₆ to C₁₈ alpha-olefins,still more preferably at least 80 wt % C₆ to C₁₈ alpha-olefins, and mostpreferably at least 90 wt % C₆ to C₁₈ alpha-olefins. For example, theolefinic feedstock may comprise at least 95 wt % C₆ to C₁₈alpha-olefins, at least 98 wt % C₆ to C₁₈ alpha-olefins or at least 99wt % C₆ to C₁₈ alpha-olefins.

In some embodiments, the olefinic feedstock comprises at least 30 wt %C₈ to C₁₄ alpha-olefins, more preferably at least 50 wt % C₈ to C₁₄alpha-olefins, more preferably at least 70 wt % C₈ to C₁₄ alpha-olefins,still more preferably at least 80 wt % C₈ to C₁₄ alpha-olefins, and mostpreferably at least 90 wt % C₈ to C₁₄ alpha-olefins. For example, theolefinic feedstock may comprise at least 95 wt % C₈ to C₁₄alpha-olefins, at least 98 wt % C₈ to C₁₄ alpha-olefins or at least 99wt % C₈ to C₁₄ alpha-olefins.

In more preferred embodiments, the olefinic feedstock comprises at least30 wt % C₁₀ to C₁₂ alpha-olefins, more preferably at least 50 wt % C₁₀to C₁₂ alpha-olefins, more preferably at least 70 wt % C₁₀ to C₁₂alpha-olefins, still more preferably at least 80 wt % C₁₀ to C₁₂alpha-olefins, and most preferably at least 90 wt % C₁₀ to C₁₂alpha-olefins. For example, the olefinic feedstock may comprise at least95 wt % C₁₀ to C₁₂ alpha-olefins, at least 98 wt % C₁₀ to C₁₂alpha-olefins or at least 99 wt % C₁₀ to C₁₂ alpha-olefins.

In some embodiments, the olefinic feedstock preferably comprises atleast 30 wt % 1-decene, more preferably at least 50 wt % 1-decene, morepreferably at least 70 wt % 1-decene, still more preferably at least 80wt % 1-decene, and most preferably at least 90 wt % 1-decene. Forexample, the olefinic feedstock may comprise at least 95 wt % 1-decene,at least 98 wt % 1-decene or at least 99 wt % 1-decene.

In other embodiments, the olefinic feedstock preferably comprises atleast 30 wt % 1-dodecene, more preferably at least 50 wt % 1-dodecene,more preferably at least 70 wt % 1-dodecene, still more preferably atleast 80 wt % 1-dodecene and most preferably at least 90 wt %1-dodecene. For example, the olefinic feedstock may comprise at least 95wt % 1-dodecene, at least 98 wt % 1-dodecene or at least 99 wt %1-dodecene.

In further embodiments, the olefinic feedstock may comprise at least 30wt % C₁₆ to C₁₈ alpha-olefins, more preferably at least 50 wt % C₁₆ toC₁₈ alpha-olefins, more preferably at least 70 wt % C₁₆ to C₁₈alpha-olefins, still more preferably at least 80 wt % C₁₆ to C₁₈alpha-olefins, and most preferably at least 90 wt % C₁₆ to C₁₈alpha-olefins. For example, the olefinic feedstock may comprise at least95 wt % C₁₆ to C₁₈ alpha-olefins, at least 98 wt % C₁₆ to C₁₈alpha-olefins or at least 99 wt % C₁₆ to C₁₈ alpha-olefins.

In some embodiments, the olefinic feedstock preferably comprises atleast 30 wt % 1-hexadecene, more preferably at least 50 wt %1-hexadecene, more preferably at least 70 wt % 1-hexadecene, still morepreferably at least 80 wt % 1-hexadecene, and most preferably at least90 wt % 1-hexadecene. For example, the olefinic feedstock may compriseat least 95 wt % 1-hexadecene, at least 98 wt % 1-hexadecene or at least99 wt % 1-hexadecene.

In other embodiments, the olefinic feedstock preferably comprises atleast 30 wt % 1-octadecene, more preferably at least 50 wt %1-octadecene, more preferably at least 70 wt % 1-octadecene, still morepreferably at least 80 wt % 1-octadecene and most preferably at least 90wt % 1-octadecene. For example, the olefinic feedstock may comprise atleast 95 wt % 1-octadecene, at least 98 wt % 1-octadecene or at least 99wt % 1-octadecene.

In some embodiments of the invention, the olefinic feedstock may alsocomprise paraffins. In general, the olefinic feedstock comprises a minoramount of paraffins. For instance, the olefinic feedstock may optionallycomprise up to 20 wt % paraffins, for instance up to 10 wt % paraffins,or up to 5 wt % paraffins. However, it will be appreciated that olefinicfeedstocks comprising larger amounts of paraffins are also suitable asfeedstocks for the present invention. For instance, olefinic feedstockscomprising up to 60 wt %, 70 wt %, 80 wt % or 90 wt % paraffins arefound to be suitable feedstocks for the process of the presentinvention. The presence of a minor amount of paraffins in the olefinicfeedstock is observed to suppress the formation of undesired heavyoligomers. Suitable paraffins include C₅ to C₂₀ paraffins, such as C₁₀to C₁₂ paraffins.

In preferred embodiments, the olefinic feedstock has a ratio ofcarbon-14 to carbon-12 of at least 0.5×10⁻¹³, more preferably at least0.6×10⁻¹³, more preferably at least 0.7×10⁻¹³, more preferably at least0.8×10⁻¹³, and most preferably at least 0.9×10⁻¹³, for example at least0.95×10⁻¹³.

The olefinic feedstock may suitably be contacted with the liquid complexcatalyst at a temperature of from 0° C. up to the boiling point of thealpha-olefins at the reaction pressure. Preferably, the olefinicfeedstock is contacted with the liquid complex catalyst at a temperatureof from 0 to 160° C., more preferably 40 to 140° C., more preferably 80to 140° C., still more preferably 100 to 140° C., and most preferablyabout 120° C. The formation of oligomers in accordance with the presentinvention is exothermic, and thus a cooling system may be used so as tomaintain the desired reaction temperature.

The olefinic feedstock may suitably be contacted with the liquid complexcatalyst at a pressure of from 10 to 1000 kPa, preferably from 20 to 500kPa, more preferably from 50 to 200 kPa, for instance from 80 to 120kPa. Preferably, the olefinic feedstock is contacted with the liquidcomplex catalyst at ambient pressure, i.e. around 100 kPa.

The olefinic feedstock may suitably be contacted with the liquid complexcatalyst for a period of from 1 minute to 10 hours, for example from 10minutes to 1 hour.

The reaction is preferably carried out under an inert atmosphere andsubstantially in the absence of moisture, defined as less than 800 ppmby weight water based on the total weight of liquid complex catalyst andolefinic feedstock.

The process of the present invention may suitably be carried out bycontacting the olefinic feedstock with at least 0.01 wt % of the liquidcomplex catalyst, more preferably at least 0.05 wt % of the liquidcomplex catalyst, still more preferably at least 0.1 wt % of the liquidcomplex catalyst, and most preferably at least 0.2 wt % of the liquidcomplex catalyst, based on the total weight of the liquid complexcatalyst and olefinic feedstock. For example, the olefinic feedstock maysuitably be contacted with from 0.01 to 5 wt % of the liquid complexcatalyst, preferably from 0.05 to 2 wt % of the liquid complex catalyst,still more preferably from 0.1 to 1 wt % of the liquid complex catalyst,and still more preferably from 0.2 to 0.8 wt % of the liquid complexcatalyst, based on the total weight of the liquid complex catalyst andolefinic feedstock. Most preferably, the olefinic feedstock is contactedwith about 0.5 wt % of the liquid complex catalyst, based on the totalweight of the liquid complex catalyst and olefinic feedstock.

It has been found that the oligomerised product distribution is notdependent on the catalyst loading to any significant degree. However,higher catalyst loadings generally reduce the reaction time and improveconversion of starting materials. Due to the exothermic nature of thereaction, the use of higher catalyst loadings may in some casesnecessitate additional measures to maintain the desired reactiontemperature.

The oligomer product obtained by the present invention may be separatedfrom the liquid complex catalyst by any suitable means, for instance bygravity separation and decantation or by centrifugation. Alternatively,the reaction may be quenched by the addition of water, optionallycontaining a mild base, and the organic and aqueous phases may beseparated, for instance by gravity separation and decantation or bycentrifugation.

The oligomerised product obtained by the process of the presentinvention typically contains minor amounts of highly oligomerisedproducts (defined herein as hexamers and higher oligomers) as well asunreacted starting material. In some embodiments, the process of theinvention may further comprise distillation of the oligomerised productto separate starting material and/or highly oligomerised products fromthe desired lower oligomers (defined herein as dimers, trimers,tetramers and pentamers).

The catalytic oligomerisation of alpha-olefins generally providesoligomerised products that contain one remaining double bond. Thepresence of double bonds generally reduces the oxidative stability of alubricating oil base stock. Thus, in some embodiments, the process ofthe present invention further comprises a step in which the remainingolefinic double bonds in the oligomerised product are reduced tocarbon-carbon single bonds so as to improve the oxidation stability ofthe product. Suitably, the reduction of olefinic double bonds may becarried out by hydrogenation in the presence of a suitable hydrogenationcatalyst, for instance a Group VIII metal such as platinum, palladium,nickel, rhodium or iridium on a solid support. In other embodiments, theprocess may further comprise a step in which the remaining olefinicdouble bonds in the oligomerised product are alkylated.

In preferred embodiments, the process of the present invention isselective for the preparation of dimers, trimers and tetramers. Infurther preferred embodiments, the process of the present invention isselective for the preparation of dimers and trimers. As noted above, theformation of higher oligomers may be suppressed, if required, by theinclusion of paraffins in the olefinic feedstock.

The oligomerised products produced according to the process of thepresent invention have a range of desirable properties.

In some embodiments, the oligomerised products produced according to theprocess of the present invention have a Kv40 of from 5 to 60 cSt,preferably from 10 to 40 cSt.

In some embodiments, the oligomerised products produced according to theprocess of the present invention have a Kv100 of from 1 to 15 cSt,preferably from 1.5 to 10 cSt, more preferably from 1.5 to 8.5 cSt (suchas 2, 4, 6 or 8), still more preferably from 3.5 to 8.5 cSt (such as 4,6 or 8), and most preferably from 3.5 to 6.5 cSt (such as 4 or 6).

In some embodiments, the oligomerised products produced according to theprocess of the present invention have a pour point of −20° C. or less,preferably of −30° C. or less (in accordance with ASTM D97-11).

In some embodiments, the oligomerised products produced according to theprocess of the present invention have a viscosity index (VI) of 100 orgreater, more preferably from 120 to 160 (according to ASTM D2270)

In another aspect, the present invention provides a compositioncomprising or consisting of alpha-olefin oligomers wherein saidcomposition is obtainable by a process as defined above.

It has surprisingly been found by the inventors that products of thepresent invention can be discerned from polyalphaolefin productspreviously reported in the art. More specifically, the products of thepresent invention can be distinguished from prior art polyalphaolefinsby analysis of their carbon-14 content.

Accordingly, in another aspect, the present invention provides acomposition comprising or consisting of polyalphaolefin oligomersobtainable by oligomerising an olefinic feedstock comprising C₅ to C₂₀alpha-olefins, wherein the ratio of carbon-14 to carbon-12 in saidcomposition is at least 0.5×10⁻¹³. In accordance with this aspect of theinvention, the ratio of carbon-14 to carbon-12 in said composition ispreferably at least 0.6×10⁻¹³, more preferably at least 0.7×10⁻¹³, morepreferably at least 0.8×10⁻¹³, and most preferably at least 0.9×10⁻¹³,for example at least 0.95×10⁻¹³.

The ratio of carbon-14 to carbon-12 in the composition of the inventionmay also be defined relative to the ratio of carbon-14 to carbon-12 inthe atmosphere. Thus, in accordance with preferred embodiments of theinvention, the ratio of carbon-14 to carbon-12 in the composition of theinvention is at least 50% of the ratio of carbon-14 to carbon-12 in theatmosphere, more preferably at least 60% of the ratio of carbon-14 tocarbon-12 in the atmosphere, more preferably at least 70% of the ratioof carbon-14 to carbon-12 in the atmosphere, still more preferably atleast 80% of the ratio of carbon-14 to carbon-12 in the atmosphere,still more preferably at least 90% of the ratio of carbon-14 tocarbon-12 in the atmosphere, and most preferably at least 95% of theratio of carbon-14 to carbon-12 in the atmosphere.

It is believed that the compositions of the present invention may bedistinguished from fossil-fuel derived olefin feedstocks on the basisthat bio-derived products produced by the processes of the presentinvention contain measurable amounts of the unstable radioisotopecarbon-14. Carbon-14 is produced in the atmosphere by the interaction ofcosmic radiation with atmospheric nitrogen. When plants absorbatmospheric carbon dioxide during photosynthesis, both carbon-12 andcarbon-14 are incorporated into carbohydrates, and subsequently intofatty acids. In living organisms, the ratio of carbon-14 to carbon-12 isapproximately equal to that of atmospheric carbon dioxide (about1.0×10⁻¹²).

Carbon-14 has a half-life of 5730±40 years and is present in detectableamounts in plant-derived carbonaceous products for a period of about60,000 years from biosynthesis. While fossil fuels are ultimatelyderived from organic matter, the carbon content of fossil fuels is ofthe order of several million years old (up to 650 million years) andtherefore the amount of residual carbon-14 falls far below the limits ofdetection.

In preferred embodiments, the composition of the invention may beobtained by oligomerising any of the olefinic feedstocks describedabove, such as feedstocks having a ratio of carbon-14 to carbon-12 inthe olefinic feedstock of at least 0.5×10⁻¹³, preferably at least0.6×10⁻¹³, more preferably at least 0.7×10⁻¹³, more preferably at least0.8×10⁻¹³, and most preferably at least 0.9×10⁻¹³, for example at least0.95×10⁻¹³.

In preferred embodiments, the composition of the invention comprises atleast 50 wt % lower oligomers, more preferably at least 60 wt % loweroligomers, still more preferably at least 70 wt % lower oligomers, andmost preferably at least 80 wt % lower oligomers, wherein loweroligomers are defined as dimers, trimers, tetramers and pentamers ofalpha-olefins.

In some embodiments, the composition of the invention has a Kv40 of from5 to 60 cSt, preferably from 10 to 40 cSt.

In some embodiments, the composition of the invention has a Kv100 offrom 1 to 15 cSt, preferably from 1.5 to 10 cSt, more preferably from1.5 to 8.5 cSt (such as 2, 4, 6 or 8), still more preferably from 3.5 to8.5 cSt (such as 4, 6 or 8), and most preferably from 3.5 to 6.5 cSt(such as 4 or 6).

In some embodiments, the composition of the invention has a pour pointof −20° C. or less, preferably of −30° C. or less (in accordance withASTM D97-11).

In some embodiments, the composition of the invention has a viscosityindex (VI) of 100 or greater, more preferably from 120 to 160 (accordingto ASTM D2270).

The present invention will now be illustrated by reference to thefollowing Examples and the accompanying figures, in which:

FIG. 1 shows the overlaid ²⁷Al NMR spectra for LC compositions obtainedfrom AlCl₃ and acetamide (AcA) where χ_(AlCl3) is 0.50 and 0.60.

FIG. 2 shows the simulated distillation (SimDist) analysis of theproduct distribution obtained by oligomerising 1-decene in the presenceof [C₂mim][Al₂Cl₇] (i.e. [C₂mim]Cl-AlCl₃, χ_(AlCl3)=0.67).

FIG. 3 shows the SimDist analysis of the product distribution obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (Ur) (χ_(AlCl3)=0.60). The product distribution obtained using[C₂mim][Al₂Cl₇] is also shown for reference.

FIG. 4 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of LCs prepared from AlCl₃ anda ligand selected from urea (Ur), trioctylphosphine oxide (P₈₈₈O),dimethylthiourea (SUr), and acetone (Act) (χ_(AlCl3)=0.60 in each case).

FIG. 5 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of LCs prepared from AlCl₃ anda ligand selected from urea (Ur), ethyl acetate (EtOAc),dimethylsulfoxide (DMSO) and dimethylacetamide (DMA) (χ_(AlCl3)=0.60 ineach case).

FIG. 6 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of LCs prepared from AlCl₃ anda ligand selected from acetamide (AcA), urea, a 1:1 binary mixture ofacetone and urea, and a 1:1 binary mixture of acetamide and urea,(χ_(AlCl3)=0.60 in each case).

FIG. 7 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (χ_(AlCl3)=0.60) at a range of temperatures.

FIG. 8 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (χ_(AlCl3)=0.60) with catalyst loadings of 1.85 mol % and 0.19wt %.

FIG. 9 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (χ_(AlCl3)=0.60) with reaction times of 10 minutes and 150minutes.

FIG. 10 shows the gas chromatograms of the products obtained byoligomerising pure 1-decene and 10 mol % 1-decene in decane in thepresence of a LC prepared from AlCl₃ and urea (χ_(AlCl3)=0.60).

FIG. 11 shows the SimDist analyses of the product distributions obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (χ_(AlCl3)=0.55) in parallel reactions.

FIG. 12 shows the gas chromatogram of the product obtained byoligomerising 1-decene in the presence of a LC prepared from AlCl₃ andurea (χ_(AlCl3)=0.60) compared to the gas chromatograms of commercialPAOs.

FIG. 13 shows the SimDist analysis of the product distribution obtainedby oligomerising 1-decene in the presence of a LC prepared from AlCl₃and urea (χ_(AlCl3)=0.60) compared to the SimDist analyses of commercialPAOs.

FIG. 14 shows the gas chromatograms of the products obtained byoligomerising C₁₆ alpha-olefins, C₁₆ alpha-olefins diluted with decane(1:1 by volume) and C₁₈ alpha-olefins in the presence of a LC catalystprepared from AlCl₃ and urea (χ_(AlCl3)=0.60).

FIG. 15 shows the SimDist analysis of the product distribution obtainedby oligomerising 1-hexadecene in the presence of the ionic liquid[C₂mim][Al₂Cl₇] compared to the product distribution obtained using a LCcatalyst prepared from AlCl₃ and urea (Ur) (χ_(AlCl3)=0.60).

EXAMPLES Reference Example 1 Synthesis of [C₂mim][Al₂Cl₇]

The ionic liquid 1-ethyl-3-methylimidazolium chloride-AlCl₃ withχ_(AlCl3)=0.67 (referred to herein as [C₂mim][Al₂Cl₇]) was prepared byslowly adding of aluminium (III) chloride (33.60 g, 0.252 mol) to[C₂mim]Cl (18.46 g, 0.126 mol) under an inert atmosphere. A clear, lightbrown, mobile ionic liquid was generated in the course of an exothermicreaction.

Example 2 Synthesis of AlCl₃-Urea Liquid Complexes

LCs having χ_(AlCl3) values of from 0.5 to 0.67 were prepared fromaluminium (III) chloride and urea by slowly adding 1 molar equivalent ofurea to 1 to 2 molar equivalents of aluminium (III) chloride withstirring under an inert atmosphere. Once addition of the urea ligand wascomplete, the resulting mixture was stirred at 80° C. for 1 hour toprovide a homogeneous, mobile, colourless liquid. The LCs were storedunder an inert atmosphere until used.

Example 3 Synthesis of Other Liquid Complexes

LCs containing ligands selected from dimethylacetamide,trioctylphosphine oxide, dimethyl sulfoxide, ethyl acetate,N,N′-dimethylthiourea, acetone and acetonitrile and each havingχ_(AlCl3)=0.60 were prepared by an analogous procedure to Example 2,using 3 molar equivalents of aluminium (III) chloride and two molarequivalents of the ligand. The properties of the different liquidcomplexes are described in Table 1.

TABLE 1 Ligand Result Dimethylacetamide Colourless, mobile liquidTrioctylphosphine oxide Yellow, slightly viscous liquid Dimethylsulfoxide Dark brown, mobile liquid Ethyl acetate, Yellow, mobile liquidN,N′-dimethylthiourea Colourless, mobile liquid Acetone Yellow, mobileliquid Acetonitrile Room temperature solid, melting point ca. 80° C.

Example 4 Generic Procedure for Oligomerisation Reactions

Oligomerisation reactions were conducted in a battery ofcomputer-controlled reactors, each having a volume of 120 mL. Due to thecorrosive nature of the catalyst, the reactors are designed for highcorrosion resistance, with the sample remaining in contact only withglass, Teflon™ and Hastelloy™. Prior to the reaction, the reactorvessels and stirrer propellers are dried overnight in an oven, andsubsequently cooled to ambient temperature in a desiccator containingphosphorus(V) oxide. The remaining parts are dried with a heat gunimmediately before assembly.

1-Decene (40 mL, dry by Karl-Fisher analysis) is added to each reactorvessel and the reactors are purged with dry argon. The reactors are thenequilibrated to the required reaction temperature with vigorous stirring(600 rpm).

Immediately prior to use, the liquid complex or ionic liquid is loadedinto a gas-tight syringe in a glovebox. Prior to use, the syringe isdried overnight in an oven, cooled in a desiccator and then transferreddirectly to the glovebox. The tip of the needle is plunged into a smallflask closed with a septum to protect it from contact with theatmosphere. Subsequently, the loaded syringe is removed from theglovebox and the needle is immediately plunged through a septum into areactor containing the 1-decene feedstock at the required reactiontemperature and stirred at 600 rpm.

The liquid complex or ionic liquid catalyst is added drop-wise to thevigorously stirred feedstock as quickly as possible, but maintaining asubstantially constant reaction temperature (i.e. avoiding exothermsgreater than 10° C.). After stirring at the required reactiontemperature for the specified reaction time, the reaction mixture isquenched by vigorous stirring (600 rpm, 10 min, ambient temperature)with deionised water (30 mL). Aqueous ammonia (10%, 10 mL) added and themixture is subsequently centrifuged to fully partition the aqueous andorganic phases.

The boiling point distribution of oligomerised products was generated bysimulated distillation (SimDist) according to ASTM 6352. Simulateddistillation is a technique widely used in the petroleum industry forevaluation of hydrocarbon products in which the boiling pointdistribution of a mixture of hydrocarbons is calibrated to the gaschromatographic analysis of the mixture. Samples of SimDist analysiswere dissolved in toluene (100 mg·cm⁻³), dried over magnesium sulphateand filtered prior to analysis. SimDist analyses are shown as cumulativedistributions with the maximum molecular weight of the oligomerssuitable for use as lubricant base stocks indicated by a horizontal lineat a boiling point of ca. 580° C. Highly oligomerised products having aboiling point above 580° C. are referred to herein as “heavies”.

Pour points were measured in accordance with ASTM D97-11 or by asimulation thereof using a series of ice salt and dry ice-solvent bathsfrom 0° C. down to −51° C.

Kinematic viscosity (Kv) is measured at 40° C. and 100° C. using theappropriate Cannon-Fenske kinematic viscosity glassware and a dedicated,precisely-controlled heating bath. Kinematic viscosity is found bytiming the gravitational flow of the sample through a capillary, withtemperature maintained using a high accuracy heating bath.

In order to select appropriate Cannon-Fenske tubes, dynamic viscosity ofsome samples was measured using Bohlin Gemini cone-and-plate viscometerwith a Bohlin Instruments Peltier temperature control and a stainlesssteel 4/40 spindle. Dynamic viscosity was measured within a temperaturerange of 20-95° C., in 5° C. increments. From dynamic viscosity (μ) anddensity (ρ) kinematic viscosity, Kv was estimated using the followingrelationship: Kv≈μρ−1, to select the appropriate Cannon-Fenske tubes.

Viscosity Index (VI) was calculated from the measured Kv40 and Kv100values according to ASTM D2270.

Reference Example 5 Oligomerisation of 1-Decene Using [C₂mim]Cl—AlCl₃(χ_(AlCl3)=0.55)

Oligomerisation of 1-decene was carried out in the presence of 1.5 wt %of the ionic liquid of Reference Example 1 according to the generalprocedure of Example 4 with a reaction temperature of 120° C. and areaction time of 20 minutes. The results of the SimDist analysis areprovided in FIG. 2. While the conversion of starting materials is foundto be very high, the oligomeric product obtained using this ionic liquidcontains a large proportion of highly oligomerised products, withapproximately 80 wt % of the products in the heavies range.

Example 6 Oligomerisation of 1-Decene Using LC Catalyst

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of a LC catalyst prepared fromAlCl₃ and urea (Ur), (χ_(AlCl3)=0.60). The reaction was carried out at120° C. for a period of 20 minutes using 1.85 wt % of the LC catalyst.

The SimDist results are provided in FIG. 3 (the results for ReferenceExample 5 are also shown in FIG. 3 for reference). It is found that theLC system of the present invention provides oligomerised products withconversions of starting material as high as 85 wt % and with far lowerproduction of heavies than the ionic liquid system of Reference Example5. Numerical results are also provided in Table 2 below (see Example 7).

Example 7 Oligomerisation of 1-Decene Using LC Catalysts

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of LC catalysts prepared fromAlCl₃ and a ligand selected from trioctylphosphine oxide (P₈₈₈O),dimethylthiourea (SUr), acetone (Act), ethyl acetate (EtOAc),dimethylsulfoxide (DMSO) and dimethylacetamide (DMA) with χ_(AlCl3)=0.60in each case. The reactions were carried out at 120° C. for a period of20 minutes using 1 mol % (ca. 1.8 wt %) of the LC catalyst.

The SimDist results are provided in FIGS. 4 and 5 (the results for ureaare shown in both Figures for reference). It is found that the LCsystems of the present invention provide oligomerised products withconversions of starting material as high as 85 wt % and with far lowerproduction of heavies than the ionic liquid system of Reference Example5. Numerical results are also provided in Table 2.

TABLE 2 Conversion C20 C30 C40 C50 C60 C70+ Ligand mass % mass % ofproduct Ur 71.0 47.1 38.6 11.4 2.9 — — DMSO 82.0 28.4 32.1 23.5 11.1 4.9— EtOAc 82.0 27.2 33.3 21.0 9.9 6.2 2.5 Act 85.0 21.4 32.1 22.6 13.1 6.04.8 SUr 22.0 14.3 33.3 28.6 19.0 4.8 — P₈₈₈O 74.0 35.6 43.8 16.4 4.1 — —DMA 80.0 27.8 29.1 21.5 12.7 6.3 2.5

Example 8 Oligomerisation of 1-Decene Using Further LC Catalysts

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of further LC catalysts preparedfrom AlCl₃ and a ligand selected from acetamide (AcA), urea, a 1:1binary mixture of acetone and urea, and a 1:1 binary mixture ofacetamide and urea, with χ_(AlCl3)=0.60 in each case. The reaction timeswere 1 hour for the LC containing only acetamide as a ligand and 20minutes in all other cases. The reaction temperature was 80° C. for theLC containing a 1:1 mixture of acetone and urea, and the catalystloading was 2.77 wt %. In all other cases a temperature of 100° C. and acatalyst loading of 1.85 wt % was used. The SimDist results are providedin FIG. 6. The result obtained at 80° C. indicates that lowertemperatures provide a greater proportion of heavy oligomers.

Example 9 Temperature Dependence of LC Catalysed Oligomerisation of1-Decene

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of 1.85 wt % of a LC catalystprepared from AlCl₃ and urea (χ_(AlCl3)=0.60). The reactions werecarried out at 120° C., 130° C. and 140° C. and over a period of 20minutes in each case. The SimDist results are provided in FIG. 7. Withinthis temperature range, no significant variation in results wasobserved.

Example 10 Effect of Catalyst Loading in the LC CatalysedOligomerisation of 1-Decene

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of a LC catalyst prepared fromAlCl₃ and urea (χ_(AlCl3)=0.60) and with catalyst loadings of 0.19 wt %and 1.85 wt %. The reaction was carried out at 140° C. and over a periodof 20 minutes in the case of 1.85 wt % catalyst loading, and over aperiod of 30 minutes in the case of 0.19 wt % catalyst loading. TheSimDist results are provided in FIG. 8. No significant difference inconversion was observed.

Example 11 Effect of Reaction Time in the LC Catalysed Oligomerisationof 1-Decene

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of a LC catalyst prepared fromAlCl₃ and urea (χ_(AlCl3)=0.60) and over a period of 10 minutes and 150minutes. The reaction temperature was 120° C. in each case and thecatalyst loading was 0.93 wt %. The SimDist results are provided in FIG.9. Although the reaction time was increased by a factor of 15, only asmall increase in conversion was observed. The product distribution issubstantially unchanged, however, with only a low level of heaviesproduced. The physical properties of the oligomeric product afterremoval of monomer and most of the dimer are provided in Table 3.

TABLE 3 Reaction time conversion Kv₄₀ Kv₁₀₀ VI 150 82 33.5271 5.7535 11310 73 24.6905 4.7272 110

Example 12 Effect of Paraffins in the Feedstock in the LC CatalysedOligomerisation of 1-Decene

Oligomerisation of 1-decene in the form of a mixture of 10 wt % decenein decane was carried out according to the general procedure of Example4 in the presence of 1.85 wt % of a LC catalyst prepared from AlCl₃ andurea (χ_(AlCl3)=0.60) and at a reaction temperature of 120° C. over aperiod of 20 minutes. The results are provided in FIG. 10 in the form ofa gas chromatography (GC) trace alongside the result obtained using only100% 1-decene as the feedstock under corresponding conditions. Thepresence of decane is observed to shift the product distribution towardsshorter oligomers.

Example 13 Reproducibility of the LC Catalysed Oligomerisation of1-Decene

Oligomerisation of 1-decene according to the general procedure ofExample 4 was carried out in triplicate in the presence of 3.71 wt % ofa LC catalyst prepared from AlCl₃ and urea (χ_(AlCl3)=0.55). Thereaction temperature was 80° C. and the reaction was conducted over aperiod of 1 hour. The SimDist results are provided in FIG. 11 and showexcellent reproducibility, with minor variations in conversion believedto be due to the presence of trace amounts of water.

Example 14 Comparison to Commercial PAOs

The product of the oligomerisation of 1-decene prepared according to thegeneral procedure of Example 4 in the presence of 0.93 wt % of a LCcatalyst prepared from AlCl₃ and urea (χ_(AlCl3)=0.60) at 120° C. andwith a reaction time of 1 hour, was compared to commercial samples ofPAO 4, 6 and 8. The product distribution of the oligomerised productobtained according to the process of the invention, following theremoval of unreacted monomer and most of the dimer by distillation, wasfound to correspond closely to the product distribution of commercialPAOs, as shown by the GC traces in FIG. 12 and the SimDist results inFIG. 13.

Example 15 Oligomerisation of Mixed Alpha-Olefins Using LC Catalysts

An industrial alpha-olefin feedstock having a composition of 30%1-decene, 50% 1-dodecene, 2% 1-tridecene, 12% 1-pentadecene and 6% C₁₈1-octadecene was carried out according to the general procedure ofExample 4 in the presence of a LC catalyst prepared from AlCl₃ and urea(χ_(AlCl3)=0.60) and at a range or reaction times, catalyst loadings andreaction temperatures. Due to the presence of higher alpha-olefins,lower reactivity and therefore the need for a more active system wasanticipated. In view of the composition of the feedstock, the productwould be expected to contain oligomers of various carbon numbers.Reaction conditions examined and the product distributions obtained aresummarised in Table 4

TABLE 4 Reaction Catalyst time loading Temp. <C15 C15-C25 C26-C35C36-C45 C46-C55 min wt % ° C. wt % wt % of product 120.0 0.19 120 76.020.0 3.0 1.0 0.0 120.0 0.37 120 54.0 24.0 10.0 6.0 2.0 120.0 0.37 12054.0 26.0 12.0 6.0 2.0 120.0 0.37 120 53.0 26.0 12.0 7.0 2.0 120.0 1.85120 30.0 27.0 23.0 14.0 6.0 60.0 5.56 140 14.0 26.0 31.0 28.0 1.0

As shown in Table 4, optimum conversion and product distribution wasobtained at 140° C. and with a catalyst concentration of 3 mol %.

Example 16 Oligomerisation of C₁₆ Olefinic Feedstocks

The oligomerisation of 1-hexadecene was carried out according to thegeneral procedure of Example 4 in the presence of a LC catalyst preparedfrom AlCl₃ and urea (χ_(AlCl3)=0.60) and at a range or reaction times,catalyst loadings and reaction temperatures. Heavier alpha-olefins areless chemically active than alpha-olefins of lower molecular weight.Oligomerisation of heavier alpha-olefins is therefore expected torequire a more active catalytic system. Reaction conditions examined andthe product distributions obtained are summarised in Table 5.

TABLE 5 Reaction Catalyst con- tetra- time loading temp. version dimertrimer mer >tetramer min wt % ° C. wt % wt % of product 30.0 0.5 70 82.08.6 40.7 28.4 22.2 30.0 1.74 120 76.0 48.0 40.0 10.7 1.0 15.0 1.74 14075.0 55.4 36.5 8.1 0.0 30.0 1.74 140 75.0 60.8 33.8 5.4 0.0 120.0 1.74140 86.0 49.4 40.0 9.4 1.2 120.0 3.48 140 89.0 45.5 43.2 10.2 1.1 15.03.48 140 80.0 55.7 38.0 6.3 0.0 30.0 1.74 160 81.0 57.5 36.3 6.3 0.0

Example 17 Oligomerisation of C₁₈ Olefinic Feedstocks

The oligomerisation of 1-octadecene was carried out according to thegeneral procedure of Example 4 in the presence of a LC catalyst preparedfrom AlCl₃ and urea (χ_(AlCl3)=0.60) and at a range or reaction times,catalyst loadings and reaction temperatures. Reaction conditionsexamined and the product distributions obtained are summarised in Table6.

TABLE 6 Reaction Catalyst con- tetra- time loading temp. version dimertrimer mer >tetramer min wt % ° C. wt % wt % of product 15.0 1.55 14077.0 55.3 36.8 7.9 0.0 15.0 3.09 140 78.0 53.2 39.0 7.8 0.0 20.0 0.21160 43.0 78.6 21.4 2.4 0.0 20.0 1.03 160 50.0 53.1 34.7 12.2 0.0

Example 18 Oligomerisation of Mixed C₁₆ and C₁₈ Olefinic Feedstocks

The oligomerisation of a 1:1 mixture by volume of 1-hexadecene and1-octadecene was carried out according to the general procedure ofExample 4 in the presence of a LC catalyst prepared from AlCl₃ and urea(χ_(AlCl3)=0.60) at a catalyst concentration of 1.64 wt %. The reactiontemperature was 140° C. and the reaction was carried out over a periodof 60 minutes. Analysis of the product by SimDist showed 74.0%conversion of starting material and a product distribution of 57.7 wt %dimer, 35.6 wt % trimer and 6.8 wt % tetramer. The formation of higheroligomers was not observed.

Example 19 Oligomerisation of C₁₈ Olefinic Feedstocks

The oligomerisation of a 1:1 mixture by volume of 1-hexadecene anddecane was carried out according to the general procedure of Example 4in the presence of a LC catalyst prepared from AlCl₃ and urea(χ_(AlCl3)=0.60) at a catalyst concentration of 1.64 wt %. The reactiontemperature was 140° C. and the reaction was carried out over a periodof 20 minutes. Analysis of the product by SimDist showed 80.0%conversion of starting material and a product distribution of 59.0 wt %dimer and 41.0 wt % trimer. The presence of the paraffin decane in thereaction mixture is thus observed to suppress the formation of tetramersand higher oligomers from C₁₆ alpha-olefins. The SimDist gaschromatograms for products obtained according to Examples 16, 17 and 19are provided as FIG. 14.

Reference Example 20 Oligomerisation of 1-Hexadecene Using[C₂mim][Al₂Cl₇]

Oligomerisation of 1-decene was carried out in the presence of 1.5 wt %of the ionic liquid of Reference Example 1 according to the generalprocedure of Example 4 with a reaction temperature of 120° C. and areaction time of 20 minutes. The results of the SimDist analysis areprovided in FIG. 15.

Example 21 Oligomerisation of 1-Hexadecene Using LC Catalyst

Oligomerisation of 1-hexadecene was carried out according to the generalprocedure of Example 4 in the presence of a LC catalyst prepared fromAlCl₃ and urea (Ur), (χ_(AlCl3)=0.60). The reaction was carried out at120° C. for a period of 20 minutes using 1.5 wt % of the LC catalyst.The results of the SimDist analysis are provided in FIG. 15 alongsidethe results for Reference Example 20. It is found that the LC system ofthe present invention provides an improved product distribution comparedto the ionic liquid system.

Example 22 Physical Properties of Oligomeric Products

Oligomerisation of 1-decene was carried out according to the generalprocedure of Example 4 in the presence of a LC catalyst prepared fromAlCl₃ and urea at a range of χ_(AlCl3) values, reaction times andcatalyst loadings. The reaction temperature was 120° C. in each case.The physical properties of the oligomeric products obtained afterremoval of 1-decene monomer and most of the dimer are provided in Table7.

TABLE 7 Time Catalyst Kv₄₀ Kv₁₀₀ Pour Point χ_(AICI3) min mol % cSt cStVI ° C. 0.550 20.0 1.000 25.4610 5.0124 125 <−43 0.550 60.0 0.50024.6813 5.0124 133 <−43 0.600 60.0 0.500 27.2205 5.0796 115 <−43 0.57540.0 0.750 27.5310 5.2404 124 <−43 0.600 20.0 0.500 23.1840 4.4741 104<−43 0.575 40.0 0.750 26.4056 5.0693 121 <−43 0.575 40.0 0.750 32.39005.9206 129 <−43 0.575 40.0 0.750 33.7870 5.9868 123 <−43 0.575 40.01.170 40.8043 6.8576 126 <−43 0.600 20.0 1.000 29.6286 5.7535 140 <−430.617 40.0 0.750 33.7870 5.8313 115 <−43 0.575 73.6 0.750 40.2845 6.7176122 <−43 0.550 20.0 0.500 24.1707 4.6806 111 <−43 0.575 6.4 0.75032.7474 5.8002 120 <−43 0.575 40.0 0.750 30.9281 5.6447 124 <−43 0.57540.0 0.330 37.1657 6.3600 122 <−43 0.575 40.0 0.750 27.5494 5.2248 123<−43 0.550 60.0 1.000 33.5271 5.8624 118 <−43 0.600 60.0 1.000 56.39838.8635 134 <−43

1. A process for the preparation of alpha-olefin oligomers, comprisingcontacting an olefinic feedstock comprising C₅ to C₂₀ alpha-olefins witha liquid complex catalyst comprising: (i) at least one metal halide saltof the formula MX₃, wherein M is selected from aluminium and gallium,and each X is independently selected chlorine, bromine and iodine; and(ii) at least one Lewis basic donor ligand containing a donor atomselected from oxygen, sulphur, nitrogen, phosphorus arsenic andselenium; wherein the molar ratio of the at least one metal halide saltto the at least one Lewis basic donor ligand is in the range of from 1:1to 4:1.
 2. A process according to claim 1, wherein the ratio ofcarbon-14 to carbon-12 in the olefinic feedstock is at least 0.5×10⁻¹³.3. A process according to claim 1 or claim 2, wherein M representsaluminium.
 4. A process according to claim 3, wherein the molar ratio ofthe at least one metal halide salt to the at least one Lewis basic donorligand is in the range of from 1:1 to 2:1.
 5. A process according toclaim 4, wherein the molar ratio of the metal halide salt to the atleast one Lewis basic donor ligand is from about 55:45 to about 65:35.6. A process according to claim 5, wherein the molar ratio of the metalhalide salt to the at least one Lewis basic donor ligand is about 3:2.7. A process according to any one of the preceding claims, wherein Xrepresents bromine or chlorine, preferably chlorine.
 8. A processaccording to claim 7, wherein MX₃ represents AlCl₃.
 9. A processaccording to any one of the preceding claims, wherein the at least oneLewis basic donor ligand is selected from ligands containing a donoratom selected from oxygen, sulphur, nitrogen and phosphorus.
 10. Aprocess according to claim 9, wherein the at least one Lewis basic donorligand is selected from the group of compounds consisting of ketones,sulfoxides, phosphine-oxides, ureas, esters, amides, ethers,thioketones, thioureas, thioamides, thioethers, amines, nitriles andphosphines.
 11. A process according to claim 10, wherein the at leastone Lewis basic donor ligand is selected from amides and ureas.
 12. Aprocess according to claim 10, wherein the at least one Lewis basicdonor ligand is selected from compounds having a formula selected fromR¹—C(O)—R¹, R¹—S(O)—R¹, R²NH—C(O)—NHR², R²NH—C(S)—NHR^(2,) R¹—C(O)—NR²₂, R¹—C(O)—OR¹, (R³)₃P(O) and R¹—CN wherein: each R¹ independentlyrepresents a C₁ to C₁₀ alkyl group, preferably a C₁ to C₆ alkyl group,more preferably a C₁ to C₃ alkyl group and most preferably a methylgroup; R² is selected from hydrogen or a C₁ to C₁₀ alkyl group, morepreferably from hydrogen or a C₁ to C₆ alkyl group, still morepreferably from hydrogen or a C₁ to C₃ alkyl group, and most preferablyfrom hydrogen or a methyl group; and R³ represents a C₄ to C₁₀ alkylgroup; wherein any of R¹, R² and R³ may optionally be substituted by oneor more fluorine atoms.
 13. A process according to claim 12, wherein theat least one Lewis basic donor ligand is selected from urea,N,N′-dimethylurea, N,N′-dimethylthiourea, acetamide, dimethylacetamide,acetone, ethyl acetate dimethylsulfoxide and trioctylphosphine oxide.14. A process according to claim 13, wherein the at least one Lewisbasic donor ligand is selected from urea and acetamide.
 15. A processaccording to claim 14, wherein the at least one Lewis basic donor ligandis urea.
 16. A process according to any one of the preceding claims,wherein the olefinic feedstock comprises at least 50 wt % of one or moreC₅ to C₂₀ alpha-olefins, more preferably at least 60 wt % of one or moreC₅ to C₂₀ alpha-olefins, more preferably at least 70 wt % of one or moreC₅ to C₂₀ alpha-olefins, more preferably at least 80 wt % of one or moreC₅ to C₂₀ alpha-olefins, more preferably at least 90 wt % of one or moreC₅ to C₂₀ alpha-olefins, and most preferably at least 95 wt % of one ormore C₅ to C₂₀ alpha-olefins.
 17. A process according to claim 16,wherein the olefinic feedstock comprises at least 50 wt % C₆ to C₁₈alpha-olefins, more preferably at least 60 wt % C₆ to C₁₈ alpha-olefins,more preferably at least 70 wt % C₆ to C₁₈ alpha-olefins, still morepreferably at least 80 wt % C₆ to C₁₈ alpha-olefins, and most preferablyat least 90 wt % C₆ to C₁₈ alpha-olefins.
 18. A process according to anyone of the preceding claims, wherein the olefinic feedstock comprises atleast 30 wt % C₈ to C₁₄ alpha-olefins, preferably at least 50 wt % C₈ toC₁₄ alpha-olefins, more preferably at least 70 wt % C₈ to C₁₄alpha-olefins, still more preferably at least 80 wt % C₈ to C₁₄alpha-olefins, and most preferably at least 90 wt % C₈ to C₁₄alpha-olefins.
 19. A process according to claim 18, wherein the olefinicfeedstock comprises at least 30 wt % C₁₀ to C₁₂ alpha-olefins,preferably at least 50 wt % C₁₀ to C₁₂ alpha-olefins, more preferably atleast 70 wt % C₁₀ to C₁₂ alpha-olefins, still more preferably at least80 wt % C₁₀ to C₁₂ alpha-olefins, and most preferably at least 90 wt %C₁₀ to C₁₂ alpha-olefins.
 20. A process according to claim 19, whereinthe olefinic feedstock comprises at least 30 wt % 1-decene, preferablyat least 50 wt % 1-decene, more preferably at least 70 wt % 1-decene,still more preferably at least 80 wt % 1-decene, and most preferably atleast 90 wt % 1-decene.
 21. A process according to claim 19, wherein theolefinic feedstock comprises at least 30 wt % 1-dodecene, preferably atleast 50 wt % 1-dodecene, more preferably at least 70 wt % 1-dodecene,still more preferably at least 80 wt % 1-dodecene and most preferably atleast 90 wt % 1-dodecene.
 22. A process according to any one of claims 1to 17, wherein the olefinic feedstock comprises at least 30 wt % C₁₆ toC₁₈ alpha-olefins, more preferably at least 50 wt % C₁₆ to C₁₈alpha-olefins, more preferably at least 70 wt % C₁₆ to C₁₈alpha-olefins, still more preferably at least 80 wt % C₁₆ to C₁₈alpha-olefins, and most preferably at least 90 wt % C₁₆ to C₁₈alpha-olefins.
 23. A process according to claim 22, wherein the olefinicfeedstock comprises at least 30 wt % 1-hexadecene, more preferably atleast 50 wt % 1-hexadecene, more preferably at least 70 wt %1-hexadecene, still more preferably at least 80 wt % 1-hexadecene, andmost preferably at least 90 wt % 1-hexadecene.
 24. A process accordingto claim 22, wherein the olefinic feedstock comprises at least 30 wt %1-octadecene, more preferably at least 50 wt % 1-octadecene, morepreferably at least 70 wt % 1-octadecene, still more preferably at least80 wt % 1-octadecene and most preferably at least 90 wt % 1-octadecene.25. A process according to any one of the preceding claims, wherein theolefinic feedstock comprises a minor amount of paraffins.
 26. A processaccording to any one of the preceding claims, wherein the olefinicfeedstock has a ratio of carbon-14 to carbon-12 of at least 0.6×10⁻¹³,preferably at least 0.7×10⁻¹³, more preferably at least 0.8×10⁻¹³, andmost preferably at least 0.9×10⁻¹³, for example at least 0.95×10⁻¹³. 27.A process according to any one of the preceding claims, wherein theolefinic feedstock has a ratio of carbon-14 to carbon-12 which is atleast 50% of the ratio of carbon-14 to carbon-12 in the atmosphere. 28.A process according to any one of the preceding claims, wherein theolefinic feedstock is contacted with the liquid complex catalyst at atemperature of from 0 to 160° C., more preferably 40 to 140° C., morepreferably 80 to 140° C., still more preferably 100 to 140° C., and mostpreferably about 120° C.
 29. A process according to any one of thepreceding claims, wherein the olefinic feedstock is contacted with theliquid complex catalyst at a pressure of from 10 to 1000 kPa, preferablyfrom 20 to 500 kPa, more preferably from 50 to 200 kPa, still morepreferably from 80 to 120 kPa, and most preferably about 100 kPa.
 30. Aprocess according to any one of the preceding claims, wherein theolefinic feedstock is contacted with at least 0.01 wt % of the liquidcomplex catalyst, more preferably at least 0.05 wt % of the liquidcomplex catalyst, still more preferably at least 0.1 wt % of the liquidcomplex catalyst, and most preferably at least 0.2 wt % of the liquidcomplex catalyst, based on the total weight of the liquid complexcatalyst and olefinic feedstock.
 31. A process according to claim 30,wherein the olefinic feedstock is contacted with from 0.01 to 5 wt % ofthe liquid complex catalyst, preferably from 0.05 to 2 wt % of theliquid complex catalyst, still more preferably from 0.1 to 1 wt % of theliquid complex catalyst, and still more preferably from 0.2 to 0.8 wt %of the liquid complex catalyst, based on the total weight of the liquidcomplex catalyst and olefinic feedstock.
 32. A process according toclaim 31, wherein the olefinic feedstock is contacted with about 0.5 wt% of the liquid complex catalyst, based on the total weight of theliquid complex catalyst and olefinic feedstock.
 33. A process accordingto any one of the preceding claims which is selective for thepreparation of dimers, trimers and tetramers.
 34. A compositioncomprising or consisting of alpha-olefin oligomers wherein saidcomposition is obtainable by a process as defined in any one of claims 1to
 33. 35. A composition comprising or consisting of polyalphaolefinoligomers, wherein said composition is obtainable by oligomerising anolefinic feedstock comprising C₅ to C₂₀ alpha-olefins, wherein the ratioof carbon-14 to carbon-12 in said composition is at least 0.5×10⁻¹³. 36.A composition according to claim 35, wherein the ratio of carbon-14 tocarbon-12 in said composition is at least 0.6×10⁻¹³, preferably at least0.7×10⁻¹³, more preferably at least 0.8×10⁻¹³, and most preferably atleast 0.9×10⁻¹³, for example at least 0.95×10⁻¹³.
 37. A compositionaccording to claim 35 or claim 36, wherein the ratio of carbon-14 tocarbon-12 in the composition of the invention is at least 50% of theratio of carbon-14 to carbon-12 in the atmosphere.
 38. A compositionaccording to any one of claims 35 to 37, wherein said composition isobtainable by oligomerising an olefinic feedstock as defined in any oneof claims 16 to
 27. 39. A composition according to any one of claims 35to 38, wherein said composition comprises at least 50 wt % loweroligomers, more preferably at least 60 wt % lower oligomers, still morepreferably at least 70 wt % lower oligomers, and most preferably atleast 80 wt % lower oligomers, wherein lower oligomers are defined asdimers, trimers, tetramers and pentamers of alpha-olefins.
 40. Acomposition according to any one of claims 35 to 39, wherein saidcomposition has a Kv40 of from 5 to 60 cSt, preferably from 10 to 40cSt.
 41. A composition according to any one of claims 35 to 40, whereinsaid composition has a Kv100 of from 1 to 15 cSt, preferably from 1.5 to10 cSt, more preferably from 1.5 to 8.5 cSt, still more preferably from3.5 to 8.5 cSt, and most preferably from 3.5 to 6.5 cSt.
 42. Acomposition according to any one of claims 35 to 41, wherein saidcomposition has a pour point of −20° C. or less, preferably of −30° C.or less.
 43. A composition according to any one of claims 35 to 42,wherein said composition has a viscosity index (VI) of 100 or greater,more preferably from 120 to 160.